Additives to enhance phosphorus compound removal in refinery desalting processes

ABSTRACT

Reactive phosphorus species can be removed or transferred from a hydrocarbon phase to a water phase in an emulsion breaking process by using a composition that contains water-soluble hydroxyacids. Suitable water-soluble hydroxyacids include, but are not necessarily limited to glycolic acid, gluconic acid, C 2 -C 4  alpha-hydroxy acids, poly-hydroxy carboxylic acids, thioglycolic acid, chloroacetic acid, polymeric forms of the above hydroxyacids, poly-glycolic esters, glycolate ethers, and ammonium salt and alkali metal salts of these hydroxyacids, and mixtures thereof. The composition may optionally include a mineral acid to reduce the pH of the desalter wash water. A solvent may be optionally included in the composition. The invention permits transfer of reactive phosphorus species into the aqueous phase with little or no hydrocarbon phase undercarry into the aqueous phase. The composition is particularly useful in treating crude oil emulsions, and in removing calcium and other metals therefrom.

CROSS-REFERENCE TO RELATED APPLICATION

This application is a continuation-in-part application from U.S. patent application Ser. No. 10/649,921 filed Aug. 27, 2003, which issued Mar. 3, 2009, as U.S. Pat. No. 7,497,943, that claims the benefit of U.S. Provisional Application No. 60/407,139 filed Aug. 30, 2002.

FIELD OF THE INVENTION

The present invention relates to methods and compositions for separating emulsions of hydrocarbons and water, and more particularly relates, in one embodiment, to methods and compositions for transferring reactive phosphorus species to an aqueous phase in an emulsion breaking process.

BACKGROUND OF THE INVENTION

In an oil refinery, the desalting of crude oil has been practiced for many years. The crude is usually contaminated from several sources, including, but not necessarily limited to:

-   -   Brine contamination in the crude oil as a result of the brine         associated with the oil in the ground;     -   Minerals, clay, silt, and sand from the formation around the oil         well bore;     -   Metals including calcium, zinc, silicon, nickel, sodium,         potassium, etc.;     -   Nitrogen-containing compounds such as amines used to scrub H₂S         from refinery gas streams in amine units, or from amines used as         neutralizers in crude unit overhead systems, and also from H₂S         scavengers used in the oilfield;     -   Iron sulfides and iron oxides resulting from pipeline and vessel         corrosion during production, transport, and storage; and     -   Reactive phosphorus species that may result from gel compounds         used in oil well stimulation.

Desalting is necessary prior to further processing to remove these compounds and other inorganic materials that would otherwise cause fouling and deposits in downstream heat exchanger equipment and/or form corrosive salts detrimental to crude oil processing equipment. Further, these phosphorus compounds and metals can act as poisons for the catalysts used in downstream refinery units. Effective crude oil desalting can help minimize the effects of these contaminants on the crude unit and downstream operations. Proper desalter operations provide the following benefits to the refiner:

-   -   Reduced crude unit corrosion.     -   Reduced crude preheat system fouling.     -   Reduced potential for distillation column damage.     -   Reduced energy costs.     -   Reduced downstream process and product contamination.

Desalting is the resolution of the natural emulsion of water that accompanies the crude oil by creating another emulsion in which about 5 percent relative wash water is dispersed into the oil using a mix valve. The emulsion mix is directed into a desalter vessel containing a parallel series of electrically charged plates. Under this arrangement, the oil and water emulsion is exposed to the applied electrical field. An induced dipole is formed on each water droplet within the emulsion that causes electrostatic attraction and coalescence of the water droplets into larger and larger droplets. Eventually, the emulsion resolves into two separate phases—the oil phase (top layer) and the water phase (bottom layer). The streams of desalted crude oil and effluent water are separately discharged from the desalter.

The entire desalting process is a continuous flow procedure as opposed to a batch process. Normally, chemical additives are injected before the mix valve to help resolve the oil/water emulsion in addition to the use of electrostatic coalescence. These additives effectively allow small water droplets to more easily coalesce by lowering the oil/water interfacial tension.

Crude oil that contains a high percent of particulate solids can complicate the desalting process. The particulate solids, by nature, would prefer to transfer to the water phase. However, much of the solids in a crude oil from a field exists in tight water-in-oil emulsions. That is, oil-wetted solids in high concentration in the crude may help form tight oil and water emulsions that are difficult to resolve. These tight emulsions are often referred to as “rag” and may exist as a layer between the separated oil and water phases. The rag layer inside the desalter vessel may grow to such an extent that some of it will be inadvertently discharged with the water phase. This is a problem for the waste water treatment plant since the rag layer still contains a high percentage of unresolved emulsified oil.

As mentioned, much of the solids encountered during crude oil desalting consists commonly as particulates such as iron oxide, iron sulfide, sand, clay and even phosphorus-containing compounds, etc. Other metals that are desirably removed include, but are not necessarily limited to, calcium, zinc, silicon, nickel, sodium, potassium, and the like, and typically a number of these metals are present. Some of the materials may be present in a soluble form, and some may require modification through reaction such as hydrolysis or neutralization to become soluble. The metals may be present in inorganic or organic forms. In addition to complicating the desalter operation, phosphorus and other contaminants are of particular concern to further downstream processing. This includes the coking operation since iron and other metals remaining in the processed hydrocarbon yields a lower grade of coke. Removing the metals from the crude oil early in the hydrocarbon processing stages is desired to eventually yield high quality coke as well as to limit corrosion and fouling processing problems.

Several treatment approaches have been made to reduce total contaminant levels and these all center on the removal of contaminants at the desalter unit. Normally, the desalter only removes water soluble inorganic salts such as sodium or potassium chlorides. Some crude oils contain water insoluble forms of phosphorus, which are soluble or dispersed as fine particulate matter in the oil but not in water.

Additionally, many refineries in Canada and the northern US have experienced fouling of tower trays with deposits that have been analyzed to contain phosphorus. In one non-limiting theory, the source of these phosphorus deposits may be gel compounds used in oil well stimulation.

It would thus be desirable to develop a composition and method employing it that would cause most or all of reactive phosphorus species in the crude oil to transfer from the oil phase in a desalter operation, with little or no oil carryunder in the aqueous phase. Nonyl phenol resins have been used as desalting additives in the past, but these materials have come under suspicion as possible hormonal mimics and are ineffective by themselves of removing metals such as calcium or iron.

SUMMARY OF THE INVENTION

Accordingly, it is an object of the present invention to provide a composition and method of using it that would transfer a large part of the reactive phosphorus species in the crude oil to the aqueous phase in a desalter operation.

It is another object of the present invention to provide a composition and method for transferring reactive phosphorus species from a hydrocarbon into an aqueous phase in an emulsion breaking operation without causing oil undercarry into the aqueous phase.

In carrying out these and other objects of the invention, there is provided, in one form, a method of transferring at least a portion of one or more reactive phosphorus species from a hydrocarbon phase to a water phase involving adding to an emulsion of hydrocarbon and water, an effective amount of a composition to transfer the reactive phosphorus species from a hydrocarbon phase to a water phase containing at least one water-soluble hydroxyacid. The water-soluble hydroxyacid may be glycolic acid, gluconic acid, C₂-C₄ alpha-hydroxy acids, poly-hydroxy carboxylic acids, thioglycolic acid, chloroacetic acid, polymeric forms of the above hydroxyacids, poly-glycolic esters, glycolate ethers, and ammonium salt and alkali metal salts of these hydroxyacids, and mixtures thereof. The emulsion is then resolved into hydrocarbon phase and an aqueous phase, where at least a portion of the reactive phosphorus species have been transferred to the aqueous phase. This is accomplished by converting the water insoluble salt such as calcium naphthenate into a water soluble salt such as calcium glycolate.

In another non-limiting embodiment of the invention, there is provided a composition for transferring at least a portion of one or more reactive phosphorus species from a hydrocarbon phase to a water phase that includes a water-soluble hydroxyacid (as defined above, including the salts thereof), and a mineral acid.

There is provided in another non-limiting embodiment of the invention a composition for transferring at least a portion of reactive phosphorus species from a hydrocarbon phase to a water phase that includes a water-soluble hydroxyacid (as defined above, including the salts thereof) and at least one additional component that may be a hydrocarbon solvent, a corrosion inhibitor, a demulsifier, a scale inhibitor, metal chelants, wetting agents and mixtures thereof.

In still another non-limiting embodiment of the invention, there is provided a treated hydrocarbon emulsion that includes a hydrocarbon phase, a water phase, and a composition for transferring at least a portion of one or more reactive phosphorus species from the hydrocarbon phase to the water phase comprising a water-soluble hydroxyacid (as defined above, including the salts thereof).

BRIEF DESCRIPTION OF THE DRAWING

The FIGURE is a graph of various amines and ammonia partitioning across desalters as a function of pH.

DETAILED DESCRIPTION OF THE INVENTION

The inventors have discovered that the addition of glycolic acid (hydroxy-acetic acid) and other water-soluble hydroxyacids to a crude oil can significantly reduce the amount of calcium and other metals and/or amines as well as reactive phosphorus species in the hydrocarbon when it is run through a desalter in a refinery. The inventors have compared the “normal” desalting on a reference crude oil containing higher than normal amounts of calcium and found minimal calcium removal. The addition of glycolic acid in levels of up to a 5:1 ratio with calcium, results in much lower metals and/or amine content of the desalted oil. The levels of metals other than calcium such as iron, zinc, silicon, nickel, sodium and potassium are also reduced. The removal of particulate iron in the form of iron oxide, iron sulfide, etc. is a specific, non-limiting embodiment of the invention. By “removing” the metals and/or amines or reactive phosphorus species from the hydrocarbon or crude is meant any and all partitioning, sequestering, separating, transferring, eliminating, dividing, removing, of one or more metal or phosphorus species from the hydrocarbon or crude to any extent.

It has been discovered that the phosphorus-containing salts that form fouling deposits on the trays of refineries may be made by mixing alkyl phosphate esters with aluminum-containing compounds. The reaction forms a three-dimensional structure that is a basis of the gels used in oil well stimulation.

Addition of hydroxyacids such as glycolic acid will help in the hydrolysis of phosphate ester gelling compounds since esters are known to be hydrolyzed by acid catalysts and/or species. This reaction is further promoted by temperatures above about 180° F. (about 82° C.), alternatively about 200° F. (about 93° C). Thus, the addition of glycolic acid and the like into desalter wash water and heating above about 212° F. (about 100° C.) should promote the hydrolysis of phosphate esters and the like. Once hydrolyzed, the phosphate should be water soluble and can be removed in the desalter effluent water.

In particular, and not wishing to be limited to any particular theory, since the gel-forming compounds are alkyl phosphate esters, it is believed that contacting the crude oil or other hydrocarbon containing them with water acidified with a hydroxyacid, e.g. glycolic acid, at a temperature of from about 180° F. (about 82° C.) to about 350° F. (about 177° C.) will hydrolyze the ester bonds and/or extract aluminum away from the phosphorus. The resulting molecules will be phosphate or phosphoric acid which will dissolve in the wash water and/or organic alcohols that dissolve in oil or water depending on their molecular weight and polarity. Thus, the phosphorus will be removed from the hydrocarbon and reduce downstream fouling.

Being an aqueous additive, the glycolic acid is typically added to the wash water in the desalter. This improves distribution of the acid in the oil although addition to the aqueous phase should not be viewed as a requirement for the composition of the invention to work.

The composition and method of the invention will be valuable to produce high quality (i.e., high purity) coke from crude that may originally have contained high concentrations of metals and/or amines and solids and/or reactive phosphorus species, including iron-based solids. Further, the invention advances the technology by removing inorganic material from the crude oil without discharging any oil or emulsion to the waste treatment plant.

In this invention, it will be understood that the metals include, but are not necessarily limited to, those of Groups IA, IIA, VB, VIIB, VII, IIB, IVA and VA of the Periodic Table (CAS version). In another non-limiting embodiment, the metals include, but are not necessarily limited to calcium, iron, zinc, silicon, nickel, sodium, potassium, vanadium, mercury, manganese, barium, zinc, aluminum, copper, phosphorus, and combinations thereof. It is realized that phosphorus is not strictly a metal, but phosphorus compounds and species are nevertheless removed by this process. In particular, nickel and vanadium are known poisons for catalysts used in fluid catalytic cracking units (FCCUs) downstream.

The amines removed in accordance with the method of this invention may include, but are not necessarily limited to, monoethanolamine (MEA); diethanolamine (DEA); triethanolamine (TEA); N-methylethanolamine; N,N-dimethylethanolamine (DMEA); morpholine; N-methyl morpholine; ethylenediamine (EDA); methoxypropylamine (MOPA); N-ethyl morpholine (EMO); N-methyl ethanolamine, N-methyldiethanolamine and combinations thereof.

In one embodiment of the invention, the composition of the invention includes a water-soluble hydroxy acid. Hydroxy acids are defined herein as not including or exclusive of acetic acid. Acetic acid has sometimes been used to remove metals as well, but it has a high oil solubility and tends to stay with the hydrocarbon coming from the desalter. The acidity of the acetic acid can then cause corrosion problems in the crude unit. The water-soluble hydroxy acids are much more water-soluble and will not partition as much into the crude oil, thus reducing downstream concerns. They are also less volatile and do not distill into the crude unit overhead system where they can increase corrosion rates when combined with the water usually present at this location.

In one preferred, non-limiting embodiment of the invention, the water-soluble hydroxyacid is selected from the group consisting of glycolic acid, C₁-C₄ alpha-hydroxy acids, poly-hydroxy carboxylic acids, thioglycolic acid, chloroacetic acid, polymeric forms of the above hydroxyacids, glycolate ethers, poly-glycolic esters, and mixtures thereof. While thioglycolic acid and chloroacetic acid are not strictly speaking hydroxyacids, they are functional equivalents thereof. For the purposes of this invention, they are defined as hydroxyacids. The alpha substituent on the C₁-C₄ alpha-hydroxy acids may be any C₁-C₄ straight or branched alkyl group. In one non-limiting embodiment of the invention, the alpha substituent may be C₂-C₄ straight or branched alkyl group and lactic acid is not included. Gluconic acid, CH₂OH(CHOH)₄COOH, is a non-limiting but preferred polymer or oligomer of glycolic acid. The glycolate ethers may have the formula:

where n ranges from 1-10. The glycolate esters may have a formula:

where n is as above. Thioglycolic acid and the ethers of glycolic acid may have the added benefits of a higher boiling point, and possibly increased water solubility. A higher boiling point means the additive will not distill into the distillate fractions in the crude unit and cause corrosion or product quality concerns. The higher water solubility also favors removal of the additive from the crude in the desalter and reduces the amount that may reach the downstream processing units.

In particular, the definition of water-soluble hydroxyacids includes ammonium salt and alkali metal salts (e.g. sodium and potassium salts, etc.) of these hydroxyacids alone or in combination with the other water-soluble hydroxyacids mentioned. Such salts would be formed in the desalter wash water as the system's pH was adjusted with pH adjusters such as sodium hydroxide, potassium hydroxide, ammonia, and the like.

In another non-limiting embodiment the water-soluble hydroxyacids do not include citric acid, malic acid, tartaric acid, mandelic acid, and lactic acid. In yet another non-limiting embodiment of the invention, the definition of water-soluble hydroxyacids does not include organic acid anhydrides, particularly acetic, propionic, butyric, valeric, stearic, phthalic and benzoic anhydrides.

In yet another non-limiting embodiment of the invention, glycolic acid and gluconic acid may be used to remove calcium and amines, and phosphorus-containing species and thioglycolic acid may be used for iron removal, from crude oil or another hydrocarbon phase.

It is expected that the water-soluble hydroxyacids will be used together with other additives including, but not necessarily limited to, corrosion inhibitors, demulsifiers, pH adjusters, metal chelants, scale inhibitors, hydrocarbon solvents, and mixtures thereof, in a commercial process. Metal chelants are compounds that complex with metals to form chelates. In particular, mineral acids may be used since metal removal is best accomplished at an acidic pH. The use of combinations of water-soluble hydroxyacids, particularly glycolic acid or gluconic acid, and mineral acids may give the best economics in a commercial application. Suitable mineral acids for use in conjunction with the water-soluble hydroxyacids of this invention include, but are not necessarily limited to, sulfuric acid, hydrochloric acid, phosphoric acid, nitric acid, phosphorous acid, and mixtures thereof. As noted, in one embodiment of the invention, the method of this invention is practiced in a refinery desalting process that involves washing the crude emulsion with wash water. In one non-limiting embodiment of the invention, the amount of mineral acid used may be sufficient to lower the pH of the wash water to 6 or below. As noted below, in some embodiments of the invention, it may be necessary or preferred to lower the pH of the wash water to 5 or below, alternatively to 4 or below. The water-soluble hydroxyacids (and salts thereof) are expected to be useful over a wide pH range, although in some situations it may be necessary or desirable to adjust the pH to achieve the desired contaminant transfer or separation.

It will be appreciated that the necessary, effective or desired proportions of the hydroxyacid and/or the mineral acid will be difficult to predict in advance, since these proportions or dosages are dependent upon a number of factors, including, but not necessarily limited to, the nature of the hydrocarbon, the concentration of metal species, phosphorus species and/or amine to be removed, the temperature and pressure conditions of method, the particular hydroxyacid and mineral acid used, etc. In general, the more of a species, such as calcium, there is to be removed, the more of the reactive acid that must be added. Since many undesirable species are affected, a successful metal or phosphorus removal process may require more reactive acid on a stoichiometric basis than would be indicated by the concentration of only the target species. It may therefore be insufficient to only just add enough acid to get the pH below 6. Nevertheless, in order to give some sense of the proportions that may be used, in one non-limiting embodiment of the invention, the composition may comprise down to about 1 wt. % water-soluble hydroxy-acid; and up to about 20 wt. % mineral acid, preferably from about 1 to about 100 wt. % water-soluble hydroxyacid; and from about 1 to about 20 wt. % mineral acid, and most preferably from about 25 to about 85 wt. % water-soluble hydroxyacid; and from about 15 to about 75 wt. % mineral acid. In some non-limiting embodiments of the invention, the mineral acid is optional and may be omitted. In some non-limiting embodiments there may be limits to the amount of mineral acid added. In some cases it has been found that using mineral acid only, the breaking of the emulsion is made more difficult. In other non-restrictive cases, there may be danger of forming scales such as calcium phosphate or calcium sulfate with the use of mineral acids.

The additive blend of this invention is injected into the wash water before the mix valve in neat form or diluted with water, alcohol or similar solvent suitable to keep all additive components in solution. The amount of solvent used may range from about 10 to about 95 wt. %, based on the total composition, preferably from about 20 to about 10 wt. %.

The concentration of the additive blend composition of this invention to be used in the crude oil to be effective is very difficult to predict in advance since it depends on multiple, interrelated factors including, but not limited to, the composition of the crude, the desalting conditions (temperature, pressure, etc.), the flow rate of the crude and its residence time in the desalter, among others. Nevertheless, for the purposes of non-limiting illustration, the proportion of the active water-soluble hydroxyacid that may be used in the crude (not including any solvent or mineral acid) may range from about 1 to about 10,000 ppm-w, alternatively from about 1 to about 2000 ppm-w, and in another non-limiting embodiment from about 10 to about 500 ppm-w and will depend on the concentration of metal species to be removed. In the treatment of slop oil to remove metal species with the methods and compositions herein, it may be necessary to use very high dosages on the order of about 1 to about 10 wt %. It is anticipated that in some non-restrictive embodiments, the compositions and methods herein may be applied to waste oils such as lubricating oils and crankcase oils, in other non-limiting embodiments. The organic hydroxy acid reacts stoichiometrically with the organo metal and/or amine species to be removed. Thus an equivalent amount of organic hydroxy acid must be added compared to the concentration of metal species to be removed. A slight excess of the acid will ensure that the reaction goes to completion. In one non-limiting embodiment of the invention, the amount of water-soluble hydroxyacid is stoichiometric with the amount of metals and/or amines present, or greater than stoichiometric. For economic reasons the refinery may chose to leave some of the metal, phosphorus and/or amine species in the crude at an acceptably low level of contamination of hydrocarbon. In those cases the treatment level of the hydroxy acids can be correspondingly reduced.

It is most preferred, of course, that in the practice of this invention there be no oil carryunder in the aqueous phase, and that at least oil carryunder is minimized. Further, while it is preferred that all of the metals, phosphorus species and/or amines transfer to the aqueous phase, in one non-limiting theory of the invention, some of the metals and/or amines may be transferred from the oil phase into the rag. This proportion of metals and/or amines is then removed when the rag is cleaned out.

It is also most preferred, of course, that in the practice of this invention all of the metals, phosphorus species and/or amines transfer to the aqueous phase. In another non-limiting embodiment of the invention, 25% or less metal, phosphorus species and/or amine is present in the hydrocarbon phase after desalting, preferably 20% or less metal, phosphorus species and/or amine remains, most preferably only 10% or less remains. In some cases the refinery may chose to leave higher percentages of metal, phosphorus species and/or amine contaminants in the crude if the detrimental effects are judged to be economically acceptable.

The invention will be illustrated further with reference to the following Examples, which are not intended to limit the invention, but instead illuminate it further.

The following Electrostatic Desalting Dehydration Apparatus (EDDA) Test Method was employed to screen possible blend compositions. The EDDA is a laboratory test device to simulate the desalting process.

EDDA Test Method

-   1. Add 800, 600 or 400 ml of crude oil to be tested minus the     percent of wash water (depending on the number of tubes the EDDA     will hold) to a Waring blender. -   2. Add the required percentage of wash water to the blender to bring     the total volume up to 800, 600 or 400 ml. -   3. Mix at 50% speed (on the Variac) for 30 seconds. The speed can be     reduced if the ΔP on the mix valve is low. -   4. Pour the mixture into the EDDA tubes to just below the 100 ml     line. -   5. Place the tubes in the EDDA heating block that is at the desired     test temperature (99° C). -   6. Add the desired quantity of demulsifier, in ppm, to each tube.     With every test, a blank must be run for comparison purposes. -   7. Place the screw top electrode in the tubes and allow the samples     to heat for approximately 15 minutes. -   8. Tighten the caps and shake each tube 100-200 times and place back     in the heating block to reheat for five minutes. -   9. Place the electrode cover over the tubes and lock into place.     Make sure that there is good contact between the cover and the     electrode caps. -   10. Set the time for five minutes and run at 1500-3000 volts,     depending on the test requirements. -   11. At the end of the five minutes, pull the tubes out and check for     the percent water drop. Also check the quality of the interface and     the quality of the water and record it. -   12. Repeat steps 9, 10, and 11 until the desired total residence     time is achieved. -   13. Determine the best candidates and run a dehydration test on     those samples.     -   a) Fill the desired number of 12.5 ml centrifuge tubes to the         50% mark with xylene.     -   b) Use a glass syringe to pull 5.8 ml of dehydrated crude sample         from the desired level in the tube and mix in with the xylene in         the centrifuge tubes.     -   c) Centrifuge the tubes at 2000 rpm for 4 minutes.     -   d) Check for the quantity of water, emulsion, and solids that         are present in the bottom of the tube and record.         Analysis for Calcium

After completing the EDDA test, use a glass syringe and cannula (long, wide bore needle), to withdraw two 20 ml aliquots of the EDDA desalted crude oil. Abstract the oil at a level in the EDDA tube that is at 25 ml and 70 ml below the surface of the oil. The two samples (top cut and bottom cut) are each analyzed for calcium concentration by whatever appropriate method (wet ash or microwave digestion, acidification, dilution, AA or ICP analysis). A similar procedure would be used to generate oil and water samples that could be analyzed by ion chromatography for other contaminants such as amine salts and reactive phosphorus species.

The crude oil used was from an African country that has a high calcium content.

-   -   Additive A=70% glycolic acid, balance water.     -   Additive B=A blend of glycolic acid, phosphoric acid (pH         adjuster), a pyridine quaternary ammonium compound (corrosion         inhibitor), a dinonyl phenol/ethylene oxide oxyalkylate         (co-solvent), isopropyl alcohol and water.

TABLE I Sample A - 100% Crude Desalted Crude Oil* Raw Top Water Crude Phase, Interface, Phase, Ex. Metal Additive Oil, ppm ppm ppm ppm 1 Calcium A 370 30 31 1700 2 ″ B 370 76 76 1210 3 Iron A 60 14 15 113 4 ″ B 60 26 27 8 5 Zinc A 35 6 4 163 6 ″ B 35 17 16 34 7 Silicon A 37 <2 <2 6 8 ″ B 37 <2 2 7 9 Nickel A 8 9 9 <2 10 ″ B 8 9 10 <2 11 Sodium A 97 9 10 416 12 ″ B 97 13 12 404 13 Potassium A 789 31 32 4030 14 ″ B 789 34 32 3900 *Top Phase = 20 mL sample taken at 75 mL mark of 100 mL EDDA test tube. Interface = 20 mL oil sample taken near oil/water interface present in EDDA test tube.

TABLE II Sample B - 20% High Calcium Crude Blend Desalted Crude Oil Raw Top Water Addi- Crude Phase, Interface, Phase, Ex. Metal tive Oil, ppm ppm ppm ppm 15 Calcium A Emulsion Emulsion Emulsion Emulsion 16 ″ B 58  8  5 362  17 Iron A Emulsion Emulsion Emulsion Emulsion 18 ″ B 10  2 <2   3.6 19 Zinc A Emulsion Emulsion Emulsion Emulsion 20 ″ B  6  5 22 32 21 Silicon A Emulsion Emulsion Emulsion Emulsion 22 ″ B <2 11 20  2 23 Nickel A Emulsion Emulsion Emulsion Emulsion 24 ″ B  2  3  3 <2 25 Sodium A Emulsion Emulsion Emulsion Emulsion 26 ″ B 17 15  8 113  27 Potassium A Emulsion Emulsion Emulsion Emulsion 28 ″ B 79  3  4 91

From the data presented above it may be seen that the water-soluble hydroxyacid used (glycolic acid) effectively removed or transferred a variety of metals from the oil phase to the water phase. The inventive method was particularly effective on the high content metals such as calcium and potassium.

Tables III-VI provide additional data showing the transfer of various metals from a hydrocarbon phase to a water phase using the water-soluble hydroxy-acids of the invention. The various components are defined as follows (all proportions are volume percents):

-   Additive C 70% glycolic acid, 30% water -   Additive D 75% Additive C, 20% acrylic acid polymer scale inhibitor     (which alone is designated SI1), 1.8% alkyl pyridine quaternary     ammonium salt corrosion inhibitor, and 3.2% oxyalkylated alkyl     phenol surfactant -   Additive E 72% phosphorous acid scale control/pH adjuster compound,     14% oxyalkylated polyalkyleneamine, and 14% SI1. -   Additive F 10% oxalic acid, 20% thioglycolic acid, 10% glycolic     acid, 1.5% alkyl pyridine quaternary ammonium salt corrosion     inhibitor, and 58.5% water. -   DA through DF designate Demulsifiers A through F, which are all     various oxyalkylated alkylphenol resin demulsifiers. When used     together with an additive of this invention, they may be abbreviated     such as DA/D which indicates Demulsifier A is used together with     Additive D in the ppm ratio given in the next column. -   SI2 Scale Inhibitor 2 that contains diammonium ethylenediamine     tetracetic acid (EDTA). -   SI3 Scale Inhibitor 3 that contains an amine phosphonate scale     inhibitor. -   SRA1 Scale Removal Additive 1, which is a blend of an alkyl pyridine     quaternary ammonium salt corrosion inhibitor (same as in Additive D)     with phosphoric acid, glycolic acid and a demulsifier.

TABLE III EDDA Test Results, Examples 29-40 Test Test Dose Metals Analysis Ex Condition Sample Additive (ppm) Na K Mg Ca 29 EDDA. Crude A C 1000 Top Oil 2.3 11.5 <1 85 10% DI (in water) Interface 2.5 8.5 <1 68 Wash Water Water 443 4400 21.9 1560 30 EDDA. ″ lactic 1000 Top Oil 2.4 6.3 <1 37 10% DI acid (in water) Interface 1 6.5 <1 37 Wash Water Water 388 4170 22.1 1610 31 EDDA. ″ Blank none Oil 164 765 4 306 10% DI Wash Water 32 EDDA. ″ C 2000 5 19 <3 24 10% DI (in water) 5 20 <3 24 Wash Water 425 4670 24 1640 33 Blank None Oil 87 919 5.8 363 34 EDDA. ″ SRA1 2000 Top Oil 13 34 76 10% DI (in water) Interface 12 32 76 Wash Water Water 404 3900 21 1210 35 EDDA. ″ SI2 2000 Top Oil 11 14 192 10% DI (in water) Interface 7 10 191 Wash Water Water 414 4000 20 959 36 EDDA. ″ C 2000 Top Oil 9 31 30 10% DI (in water) Interface 10 32 31 Wash Water Water 416 4030 22 1700 37 EDDA. ″ SI3 2000 Top Oil 15 60 276 10% DI (in water) Interface 15 60 281 Wash Water Water 440 4190 538 38 EDDA. ″ Blank none Oil 97 789 4 370 10% DI Wash Water 39 EDDA. ″ SRA1 2000 Top Oil 15 3 8 10% DI (in water) Interface 8 4 5 Wash Water Water 113 91 6 362 40 EDDA. ″ Blank none Oil 17 79 58 10% DI Wash Water Metals Analysis Ex Fe Cu Zn Al Sb Ba V Pb Mn Ni Si P 29 51 <2 40.0 1.5 15 2.7 <1 8 10 10.0 1.3 8 40 <2 31.0 1.0 15 2.4 <1 8 8 8.0 <1 8 2.7 <0.1 3.7 0.3 <0.1 30.4 <0.1 0.6 18.2 0.2 5.5 <0.1 30 39 <2 30.0 1.2 14 2.4 <1 7 6 8.0 <1 7 38 <2 30.0 1.1 20 2.2 <1 10 6 8.0 <1 11 5.5 <0.1 9.9 0.5 <0.1 32.3 <0.1 0.6 29.4 0.3 5.3 0.1 31 49 <2 30.0 8.0 14 8.5 <1 8 11 7.0 10 8 32 16 <0.5 2.0 1.2 <0.5 0.7 <0.5 11.7 0.6 8.6 30.7 <2 16 <0.5 2.0 1.0 <0.5 0.7 <0.5 7.9 0.6 9.0 7.1 <2 93.8 0.2 162.0 1.5 0.4 33.8 0.2 3.1 56.4 1.0 5.5 2.2 33 68.6 <0.5 32.0 11.4 <0.5 8.4 <0.5 6.8 12.2 8.4 15.6 2.8 34 26 17.0 2 93 3 9.0 86 27 16.0 2 88 3 10.0 2 91 8 34.0 8 33 7 1300 35 29 7.0 6 80 12.0 45 9 28 2.0 5 84 9.0 2 6 82 164.0 11 4 58 6 36 14 6.0 94 9.0 5 15 4.0 86 9.0 4 113 163.0 2.0 31 4 57 6 3 37 49 38.0 5 82 13 9.0 14 215 51 39.0 5 95 13 10.0 7 223 13 7 50 38 60 35.0 8.0 8 48 13 8.0 37 3 39 2 5.0 73 3.0 11 11 22.0 59 3.0 20 5 3.6 32.0 12 2 516 40 10 6.0 37 2.0

TABLE IV EDDA Test Results, Examples 41-54 Test Test Dose Metals Analysis Ex Condition Sample Additive (ppm) Na K Mg Ca 41 EDDA. Crude A DA 15 Top Oil 5.9 17.1 <3 371 10% DI WW Water 626 <5 17 210 42 EDDA. ″ DB 15 Top Oil 5 13 <3 384 10% DI WW Water 705 <5 19 236 43 EDDA. ″ DC 15 Top Oil 11 32 5 443 10% DI WW Water 579 <5 15 193 44 EDDA. ″ DD 15 Top Oil 8 27 <3 368 10% DI WW Water 698 <5 17 234 45 EDDA. ″ DE 15 Top Oil 6 23 3 366 10% DI WW Water 612 <5 16 204 46 EDDA. ″ Blank None Oil 6 19 <3 361 10% DI WW Water 650 <5 18 216 47 EDDA. Crude B DA 15 Top Oil 4 <5 <3 40 10% DI WW Water 147 950 7 143 48 EDDA. ″ DB 15 Top Oil 5 <5 <3 41 10% DI WW Water 134 882 6 129 49 EDDA. ″ DC 15 Top Oil 5 <5 <3 39 10% DI WW Water 147 948 7 140 50 EDDA. ″ DD 15 Top Oil 4 <5 <3 41 10% DI WW Water 148 954 6 140 51 EDDA. ″ DE 15 6 <5 <3 46 8 10% DI WW 146 943 7 140 <0.2 52 EDDA. ″ Blank none Oil 5 <5 <3 48 10% DI WW Water 130 858 5 122 53 EDDA. Crude C C 50 Top Oil 3 <1 <1 4 10% DI WW Interface 4 <1 <1 3 Water 690 42 31 174 54 EDDA. ″ Bank none Oil 46 4 3 14 10% DI WW Metals Analysis Ex Fe Cu Zn Al Sb Ba V Pb Mn Ni Si P 41 58 <3 36.0 4.0 <3 5 <3 27 14 10.0 13 4 <0.2 <0.2 <0.2 <0.2 <0.2 7 <0.2 <0.4 <0.2 <0.2 10 <0.2 42 60 <3 36.0 5.0 <3 5 <3 22 14 10.0 9 3 <0.2 <0.2 <0.2 <0.2 <0.2 8 <0.2 <0.4 <0.2 <0.2 10 <0.2 43 88 <3 38.0 41.0 <3 6 <3 33 14 11.0 55 3 <0.2 <0.2 <0.2 <0.2 <0.2 7 <0.2 <0.4 <0.2 <0.2 8 <0.2 44 57 <3 36.0 4.0 <3 6 <3 33 14 10.0 8 4 <0.2 <0.2 <0.2 <0.2 <0.2 9 <0.2 <0.4 <0.2 <0.2 9 <0.2 45 55 <3 35.0 4.0 <3 5 <3 21 14 10.0 66 <3 <0.2 <0.2 <0.2 <0.2 <0.2 8 <0.2 <0.4 <0.2 <0.2 8 <0.2 46 54 <3 35.0 <3 <3 5 <3 20 13 9.0 8 3 <0.2 <0.2 <0.2 <0.2 <0.2 8 <0.2 <0.4 <0.2 <0.2 9 <0.2 47 7 <3 6.0 <3 <3 <3 8 24 <3 <3 6 <3 <0.2 <0.2 <0.2 <0.2 <0.2 2 <0.2 <0.4 <0.2 <0.2 2 <0.2 48 6 <3 6.0 <3 <3 <3 7 17 <3 <3 6 <3 <0.2 <0.2 <0.2 <0.2 <0.2 2 <0.2 <0.4 <0.2 <0.2 2 <0.2 49 7 <3 6.0 <3 <3 <3 7 21 <3 <3 4 <3 <0.2 <0.2 <0.2 <0.2 <0.2 1 <0.2 0.4 <0.2 <0.2 3 <0.2 50 6 <3 6.0 <3 <3 <3 7 21 <3 <3 3 <3 <0.2 <0.2 <0.2 <0.2 <0.2 1 <0.2 <0.4 <0.2 <0.2 3 <0.2 51 <3 6.0 <3 <3 <3 8 22 <3 <3 10 <3 <0.2 <0.2 <0.2 <0.2 1 <0.2 0.4 <0.2 <0.2 3 <0.2 52 6 <3 6.0 <3 <3 <3 8 23 <3 <3 6 <3 <0.2 <0.2 <0.2 <0.2 <0.2 1 <0.2 0.5 <0.2 <0.2 3 <0.2 53 2 <1 <1 1.0 <1 <1 12 <1 <1 6.0 3 3 5 <1 1.0 1.0 <1 <1 12 <1 <1 6.0 3 3 124 <1 6.0 2.0 <1 2 <1 <1 <1 <1 2 2 54 22 <1 2.0 2.0 <1 <1 11 <1 <1 6.0 4 4

TABLE V EDDA Test Results, Examples 55-67 Test Test Dose Metals Analysis Ex Condition Sample Additive (ppm) Na K Mg Ca 55 EDDA. Crude DA/D 15/50 Top Oil 6 29 3 225 4% DI WW D/G Blend Water 338 40 383 56 EDDA. Crude DE/D 15/50 Top Oil 6 30 4 249 4% DI WW D/G Blend Water 341 34 388 57 EDDA. Crude DB/D 15/50 Top Oil 11 76 4 244 4% DI WW D/G Blend Water 334 35 375 58 EDDA. Crude DA/D 25/50 Top Oil 8 30 2 216 4% DI WW D/G Blend Water 339 39 382 59 EDDA. Crude DE/D 25/50 Top Oil 4% DI WW D/G Blend Water 338 37 380 60 EDDA. Crude DB/D 25/50 Top Oil 13 33 1 206 4% DI WW D/G Blend Water 345 37 386 61 EDDA. Crude Blank None Oil 44 930 11 266 4% DI WW D/G Blend 62 EDDA. Crude DA/D 40/50 Top Oil 30 20 4 194 4% DI WW D/G Blend Water 155 18 142 63 EDDA. Crude DE/D 40/50 Top Oil 6 25 4 205 4% DI WW D/G Blend Water 341 39 292 64 EDDA. Crude DB/D 40/50 Top Oil 8 26 4 224 4% DI WW D/G Blend Water 336 34.2 287 65 EDDA. Crude DF/D 40/50 Top Oil 8 43 6 230 4% DI WW D/G Blend Water 352 33.7 297 66 EDDA. Crude DD/D 40/50 Top Oil 8 67 8 250 4% DI WW D/G Blend Water 344 33 386 67 EDDA. Crude DC/D 40/50 Top Oil 7 33 5 211 4% DI WW D/G Blend Water 352 33.2 300 Metals Analysis Ex Fe Cu Zn Al Sb Ba V Pb Mn Ni Si P 55 29 3 15.0 4.0 5 11 8.0 2 11 0.2 <0.1 <0.1 <0.1 <0.1 17.5 1.1 <0.1 8.1 <0.1 56 32 4 15.0 3.0 5 12 10.0 3 <1 0.2 <0.1 <0.1 <0.1 <0.1 17.4 1.1 <0.1 7.1 <0.1 57 30 5 14.0 2.0 5 12 8.0 2 6 0.1 <0.1 <0.1 <0.1 <0.1 17.3 1.1 <0.1 8 <0.1 58 26 7 15.0 3.0 5 11 7.0 <1 9 0.2 <0.1 <0.1 <0.1 <0.1 18.6 1.2 <0.1 9.6 <0.1 59 0.2 <0.1 <0.1 <0.1 <0.1 19 1.1 <0.1 8 <0.1 60 26 14 15.0 2.0 5 10 6.0 1 8 0.3 <0.1 <0.1 <0.1 <0.1 19 1.2 <0.1 8.9 <0.1 61 33 2 15.0 4.0 7 11 6.0 3 9 62 29 4 12.0 4.0 3 4 9 3.0 5 14 <0.1 <0.1 <0.1 <0.1 <0.1 6.8 0.6 <0.1 3.5 114 63 28 3 13.0 5.0 2 5 10 3.0 5 15 0.2 <0.1 <0.1 <0.1 <0.1 13.6 1.1 <0.1 6.9 180 64 31 8 17.0 6.0 <1 5 10 5.0 2 18 0.2 <0.1 <0.1 0.2 <0.1 13.4 1.1 <0.1 7.1 180 65 36 4 19.0 11.0 <1 5 11 6.0 3 18 0.2 <0.1 <0.1 0.2 <0.1 13.6 1 <0.1 6.8 187 66 34 3 21.0 10.0 <1 6 12 8.0 4 27 0.2 <0.1 0.2 1.0 <0.1 13.4 1 <0.1 6.7 177 67 34 4 14.0 10.0 <1 5 10 4.0 4 14 0.2 <0.1 0.2 <0.5 <0.1 13.6 1.1 <0.1 6.7 183

TABLE VI EDDA Test Results, Examples 68-83 Test Test Dose Metals Analysis Ex Condition Sample Additive (ppm) Na K Mg Ca 68 EDDA. Crude E Blank None Oil 63 1590 12.2 475 7.5% DI WW 69 EDDA. ″ DA/E 30/70 Top Oil 6.1 20.5 7.8 482 7.5% Water 212 2960 25 278 DI WW 70 EDDA. ″ DE/E 30/70 Top Oil 5.6 17.7 7.4 435 7.5% Water 215 2990 27 281 DI WW 71 EDDA. ″ DB/E 30/70 Top Oil 6 17.2 7.7 420 7.5% Water 218 3020 25.9 283 DI WW 72 EDDA. ″ DF/E 30/70 Top Oil 6.2 19.6 7.5 485 7.5% Water 229 3140 29.2 298 DI WW 73 EDDA. ″ DD/E 30/70 Top Oil 7 18.5 6.6 415 7.5% Water 230 3160 28.2 301 DI WW 74 EDDA. ″ DC/E 30/70 Top Oil 6 24.6 7.6 398 7.5% Water 227 3170 28.1 293 DI WW 75 EDDA 5.0% Crude G acetic 1000 Top Oil <0.4 12.6 2.5 22.6 DI Wash W. acid (in water) Water 116 2430 56.1 3350 76 EDDA 5.0% Crude F F 1000 Top Oil 0.8 7 3.9 190 DI Wash W. (in water) Water 113 2430 48.3 914 77 EDDA 5.0% Blend E Blank None Oil 11 320 3.3 100 DI Wash W. 78 EDDA 5.0% +Other acetic 1000 Top Oil 1.4 7.7 1.2 21.5 DI Wash W. Crude acid (in water) Water 146 3280 29.7 844 79 EDDA 5.0% 30/70 F 1000 Top Oil 3 1.2 1 24.7 DI Wash W. Refinery (in water) Water 140 3170 29.3 408 80 EDDA 5.0% Blend lactic 1000 Top Oil 2.5 25.6 1.3 32.2 DI Wash W. acid (in water) Water 121 2700 24.1 620 81 EDDA 5.0% ″ glycolic 1000 Top Oil 2.4 22.9 1.2 25.9 DI Wash W. acid (in water) Water 124 2830 25.2 700 82 EDDA 5.0% ″ SI1 1000 Top Oil 2 7.9 1.9 75 DI Wash W. (in water) Water 958 3950 14.3 301 83 EDDA 5.0% ″ Oxalic 1000 Top Oil 6.6 21.9 2.5 80 DI Wash W. acid (in water) Water 132 2970 20.3 87.4 Metals Analysis Ex Fe Cu Zn Al Sb Ba V Pb Mn Ni Si P 68 23.8 0.5 13.0 0.6 <0.4 11 <0.4 <0.4 10.4 10.6 3.9 2.9 69 25 0.8 14.5 2.1 <0.4 9.2 <0.4 <0.4 11.3 13.2 5.3 26.2 0.7 <0.1 0.1 4.0 <0.1 19.3 <0.4 <0.1 1.3 0.5 7.1 291 70 25.2 0.6 14.7 0.5 <0.4 9.4 <0.4 <0.4 11.6 13.6 2.4 25.5 0.7 <0.1 <0.1 0.1 <0.1 19.3 <0.4 <0.1 1.3 0.4 7.1 297 71 24 0.8 15.1 0.2 <0.4 8.6 <0.4 <0.4 11.3 13.8 3.4 27.2 0.6 <0.1 <0.1 <0.1 <0.1 19.8 <0.4 <0.1 1.3 0.7 7.5 294 72 24.8 0.8 14.7 0.6 <0.4 9.4 <0.4 <0.4 11.4 14.2 2.6 25.3 0.6 0.2 <0.1 <0.1 <0.1 19.8 <0.4 <0.1 1.3 0.9 7.3 313 73 24.5 0.4 14.5 <0.4 <0.4 8.9 <0.4 <0.4 11.3 13.6 3 26.6 0.6 <0.1 <0.1 <0.1 <0.1 20.1 <0.4 <0.1 1.3 0.6 7.4 317 74 23.4 <0.4 15.0 <0.4 <0.4 8.4 <0.4 <0.4 10.9 14.8 4 29.2 0.7 <0.1 <0.1 <0.1 <0.1 20.3 <0.1 <0.1 1.4 0.8 7.8 302 75 25.2 0.9 10.6 2.1 <0.4 0.6 <0.4 <0.4 2.5 11.6 1.1 4.2 72.1 0.5 43.9 <0.1 0.2 84.4 <0.1 0.2 126 0.5 5.4 0.3 76 31.8 0.7 15.2 3.0 <0.4 3.9 <0.4 <0.4 12.8 11.7 2.4 4 4.6 <0.1 0.7 <0.1 <0.1 44.5 <0.1 <0.1 6.4 <0.1 6.1 0.1 77 11.3 0.4 4.2 1.1 <0.4 2.5 <0.4 <0.4 4.1 3.5 0.7 1.5 78 3.5 <0.4 13.8 9.9 <0.4 0.9 <0.1 <0.4 <0.4 4.1 1.3 2.2 96 0.2 44.9 0.2 <0.1 14.8 <0.4 0.3 44.4 0.7 4 0.3 79 1.1 <0.4 0.6 1.0 <0.4 0.6 <0.1 <0.4 <0.4 4.0 <0.4 2.1 118 <0.1 52.4 2.2 <0.1 4.2 <0.4 <0.1 38.8 0.5 4.9 0.6 80 2 0.6 1.1 1.0 <0.4 0.9 <0.1 <0.4 1.2 3.9 1.8 2 92.5 0.3 37.2 0.7 0.1 10.3 <0.4 0.7 25.8 36.3 5 0.7 81 2.7 <0.4 0.9 1.5 <0.4 0.8 <0.1 <0.4 1.1 3.9 2.6 2.2 92.2 0.3 38.2 0.6 0.2 9.8 <0.4 0.9 27.6 30.7 4.2 0.6 82 11.1 0.5 5.0 1.1 <0.4 1.7 <0.1 <0.4 4.2 3.8 <0.4 1.9 1.4 0.3 0.6 0.3 <0.1 12.6 <0.4 <0.1 3.4 <0.1 5.4 0.1 83 11.4 0.5 4.7 1.0 <0.4 1.6 <0.1 <0.4 4.2 3.9 <0.4 2.3 <0.1 <0.1 <0.1 <0.1 <0.1 5.2 <0.4 <0.1 0.7 <0.1 5 <0.1

EXAMPLES 84-110

Examples 84-110 were conducted using the same EDDA Test Method and analytical method described above. All of the tests were conducted on the same sample of crude oil. This sample of western Canadian crude oil was from a refinery experiencing severing fouling with phosphorus-based deposits. The EDDA tests were run at 100° C. for all of the tests and 5.5% wash water was used in each test. After the crude oil was treated and processed in the EDDA, the effluent water was collected and sent for analysis to determine the ion content in solution by ICP. The oil samples were ashed using microwave digestion and the resulting aqueous solution was analyzed by ICP. The various compositions tested are given in Table VII.

TABLE VII Additive Composition Additive G 98% glycolic acid (70%)  2% Magna 240 corrosion inhibitor available from Baker Petrolite Additive H 95% gluconic acid  5% citric acid Additive J 95% glycolic acid  4% thioglycolic acid Blend X Blend of non-ionic emulsion breakers available from Baker Petrolite Blend Y Blend of non-ionic emulsion breakers available from Baker Petrolite

EXAMPLES 84-93

In these Examples, all samples were processed in the EDDA to simulate a desalting process. The first sample, Example 84, had no emulsion breaker of acid added, but was desalted. The rest of the samples except the wash water (Example 93) were treated with metals removal chemistry in addition to an emulsion breaker to help resolve the emulsion. In this study, Additive G at 20 ppm (Example 85) and in the other Examples 86, 89 and 90 effectively removed Ca and Fe from the crude oil. The treatment also reduced P content by about 25%.

TABLE VIII Ex. Sample Identification 84 Raw crude (Blank sample) 85 Treat at 20 ppm of Additive G, Desalter crude 86 Treat at 30 ppm of Additive G, Desalter crude 87 Treat at 30 ppm of Additive H, Desalter crude 88 Treat at 30 ppm of Additive J, Desalter crude 89 Treat at 20 ppm of Additive G, Effluent water 90 Treat at 30 ppm of Additive G, Effluent water 91 Treat at 30 ppm of Additive H, Effluent water 92 Treat at 30 ppm of Additive J, Effluent water 93 Wash water

TABLE IX ICP EDDA Test Results (ppm - wt/wt), Examples 84-93 Ex. Na K Mg Ca Mo Fe Cu Zn Al 84 73.5 4.7 6.8 33.8 <0.4 22.5 <0.4 2.0 <0.4 85 <0.4 0.6 0.9 0.6 <0.4 1.0 <0.4 1.1 <0.4 86 0.4 <0.4 0.9 0.9 <0.4 0.9 <0.4 1.0 <0.4 87 0.5 0.4 1.0 1.3 <0.4 1.7 <0.4 1.7 <0.4 88 0.6 0.4 0.8 0.8 <0.4 1.7 <0.4 1.2 <0.4 89 1160 77.4 74.5 428 <0.1 30.0 0.8 7.0 <0.1 90 1100 75.5 71.2 407 <0.1 26.3 1.3 15.0 <0.1 91 1180 79.2 77.0 430 <0.1 43.0 0.4 5.5 <0.1 92 1230 82.3 79.4 450 <0.1 57.3 0.9 7.7 <0.1 93 11.8 2.6 19.0 60.2 0.1 4.7 <0.1 <0.1 <0.1 Ex. Ba Be Cd Cr Pb Mn Ni B 84 4.5 <0.4 <0.4 <0.4 <0.4 <0.4 3.1 <0.4 85 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 2.9 <0.4 86 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.5 <0.4 87 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.2 <0.4 88 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.2 <0.4 89 0.3 <0.1 <0.1 <0.1 0.2 0.8 0.3 2.2 90 0.3 <0.1 <0.1 <0.1 0.5 0.8 0.5 2.1 91 0.4 <0.1 <0.1 <0.1 0.1 0.9 0.3 2.2 92 0.3 <0.1 <0.1 <0.1 0.2 1.0 0.3 2.5 93 <0.1 <0.1 <0.1 <0.1 <0.1 <0.1 <0.1 <0.1 Ex. Sr Si P S Ti V Sn 84 1.1 5.6 4.3 NR <0.4 6.9 <0.4 85 <0.4 0.5 3.0 NR <0.4 6.6 <0.4 86 <0.4 0.7 3.5 NR <0.4 7.6 <0.4 87 <0.4 0.7 3.4 NR <0.4 7.1 <0.4 88 <0.4 0.7 3.1 NR <0.4 7.1 <0.4 89 11.3 3.6 3.4 320 <0.1 <0.1 <0.1 90 10.7 3.4 3.2 310 <0.1 <0.1 <0.1 91 11.6 4.0 4.5 340 <0.1 <0.1 <0.1 92 12.1 4.1 4.6 350 <0.1 <0.1 <0.1 93 0.5 4.3 0.3 89.2 <0.1 <0.1 <0.1

EXAMPLE 94-95

In these Examples it may be seen that only 10 ppm of Additive G was required to remove most of the Ca and Fe. Again, the P seems to be reduced by about 25%.

TABLE X Ex. Sample Identification 94 Treat with Blend X @ 10 ppm-v Additive G @ 100 ppm-v Wash water rate 5.5% Mix ΔP = 12 psig Effluent water 95 Treat with Blend Y @ 10 ppm-v Additive G @ 100 ppm-v Wash water rate 5.5% Mix ΔP = 12 psig Desalter crude

TABLE XI ICP EDDA Test Results (ppm - wt/wt), Examples 94-95 Ex. Na K Mg Ca Mo Fe Cu Zn Al 94 1460 60.6 69.1 433 <0.1 76.3 2.8 8.7 1.8 95 <0.1 0.4 1.2 1.4 <0.1 2.0 <0.1 0.8 <0.1 Ex. Ba Be Cd Cr Pb Mn Ni B 94 0.2 <0.1 <0.1 <0.1 0.4 0.9 0.3 2.0 95 <0.1 <0.1 <0.1 <0.1 0.5 <0.1 3.1 1.3 Ex. Sr Si P S Ti V Sn 94 9.3 4.2 4.8 365 <0.1 <0.1 <0.1 95 <0.1 2.8 3.0 NR <0.1 6.5 0.5 NR = Not run

EXAMPLES 96-110

These Examples give the metals and phosphorus content of desalted crude and effluent water treated at several dosages (10, 15, 50, 100, 500 and 1000 ppm based on the crude) for Additive G. The wash water rate for all Examples was 5.5%, and the mix ΔP for all Examples was 12 psig. Most species were removed to the same extent at all dosages. Most of the Na, K, Ca, Fe, Cu, and Ba were removed at 10 ppm and higher. The Ni and V levels did not seem to be affected by the treatment. The Si was the only element to be more efficiently removed at higher treatment dosages. The P was removed to about 25-30% at the various dosages.

In one non-limiting theory, it may be that not all phosphorus species are the same. There may be more than one kind of phosphorus species present, and these treatments may only be removing some of them. It may be that at higher temperatures the additives herein will be more efficient at removing P compounds. Desalters typically run at about 125 to about 150° C., whereas the EDDA tests were run at 100° C.

TABLE XII Ex. Sample Identification 96 Raw crude 97 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 10 ppm-v Desalter crude 98 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 15 ppm-v Desalter crude 99 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 50 ppm-v Desalter crude 100 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 100 ppm-v Desalter crude 101 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 500 ppm-v Desalter crude 102 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 1,000 ppm-v Desalter crude 103 Treat with demulsifier Blend Y @ 10 ppm-v Lactic acid @ 100 ppm-v Desalter crude 104 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 10 ppm-v Effluent water 105 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 15 ppm-v Effluent water 106 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 50 ppm-v Effluent water 107 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 100 ppm-v Effluent water 108 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 500 ppm-v Effluent water 109 Treat with demulsifier Blend Y @ 10 ppm-v Additive G @ 1,000 ppm-v Effluent water 110 Treat with demulsifier Blend Y @ 10 ppm-v Lactic acid @ 100 ppm-v Effluent water

TABLE VI ICP EDDA Test Results (ppm - wt/wt), Examples 96-110 Ex. Na K Mg Ca Mo Fe Cu Zn Al  96 110 6.2 5.4 30.0 <0.4 22.7 0.5 1.3 1.1  97 0.7 <0.4 1.6 0.4 <0.4 0.5 <0.4 0.9 <0.4  98 1.7 <0.4 2.6 0.9 <0.4 0.6 <0.4 1.1 <0.4  99 1.8 <0.4 2.8 1.1 <0.4 1.6 <0.4 1.1 <0.4 100 0.9 <0.4 1.5 0.6 <0.4 0.5 <0.4 1.3 <0.4 101 60.5 0.4 2.9 2.6 <0.4 1.2 <0.4 0.9 <0.4 102 0.9 <0.4 1.6 0.7 <0.4 0.6 0.4 1.1 <0.4 103 1.0 <0.4 1.6 0.7 <0.4 0.7 <0.4 1.0 <0.4 104 1630 87.0 71.4 423 <0.1 47.1 0.8 9.8 1.2 105 1490 69.5 67.6 388 <0.1 48.8 <0.1 2.7 1.1 106 1370 71.2 65.5 367 <0.1 68.8 0.8 4.5 1.5 107 1290 64.3 63.0 345 <0.1 74.0 1.0 6.2 1.9 108 1520 78.3 72.2 420 <0.1 145 2.6 6.8 7.6 109 1385 67.8 66.3 372 <0.1 149 14.6 10.4 6.8 110 1370 72.4 65.0 368 <0.1 77.2 0.6 3.5 2.8 Ex. Ba Be Cd Cr Pb Mn Ni B  96 5.2 <0.4 <0.4 <0.4 <0.4 <0.4 3.5 <0.4  97 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.4 2.0  98 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.7 <0.4  99 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 4.0 <0.4 100 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.6 <0.4 101 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.9 <0.4 102 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.8 <0.4 103 <0.4 <0.4 <0.4 <0.4 <0.4 <0.4 3.8 <0.4 104 0.5 <0.1 <0.1 <0.1 0.3 0.9 0.4 5.6 105 0.5 <0.1 <0.1 <0.1 0.1 0.8 0.2 3.9 106 0.5 <0.1 <0.1 <0.1 0.2 0.9 0.2 3.2 107 0.5 <0.1 <0.1 <0.1 0.3 0.9 0.3 2.8 108 0.6 <0.1 <0.1 <0.1 0.5 1.2 0.3 3.1 109 0.6 <0.1 <0.1 <0.1 0.8 1.1 0.3 2.8 110 0.5 <0.1 <0.1 <0.1 0.2 0.9 0.2 2.7 Ex. Sr Si P S Ti V Sn  96 1.1 1.9 2.7 NR <0.4 7.9 0.6  97 <0.4 0.6 1.9 NR <0.4 7.5 0.6  98 <0.4 0.7 2.1 NR <0.4 8.3 0.6  99 <0.4 0.8 2.2 NR 1.2 8.8 0.4 100 <0.4 0.5 1.8 NR <0.4 7.9 <0.4 101 <0.4 1.1 2.2 NR <0.4 8.8 0.4 102 <0.4 0.6 2.0 NR <0.4 8.5 0.5 103 <0.4 0.7 2.0 NR <0.4 8.3 0.5 104 11.1 1.4 2.1 302 <0.1 <0.1 <0.1 105 10.4 1.4 2.2 284 <0.1 <0.1 <0.1 106 9.7 1.5 2.5 286 <0.1 <0.1 <0.1 107 9.2 1.4 2.5 268 <0.1 <0.1 <0.1 108 10.9 1.9 4.7 294 <0.1 <0.1 <0.1 109 10.0 2.1 5.5 265 <0.1 <0.1 <0.1 110 9.7 1.5 2.8 272 <0.1 <0.1 <0.1

The FIGURE presents a graph showing the partitioning across desalters of various amines and ammonia as a function of pH. The addition of water-soluble hydroxyacids of this invention such as glycolic and gluconic acid to the desalter wash water at the use rates specified herein will reduce the water's pH to the range of about 3-6.5.

In the foregoing specification, the invention has been described with reference to specific embodiments thereof, and has been demonstrated as effective in transferring metals, e.g. calcium, potassium, phosphorus, etc., and/or amines from crude oil to the aqueous phase in bench scale desalting testing, as non-limiting examples. However, it will be evident that various modifications and changes can be made thereto without departing from the broader spirit or scope of the invention as set forth in the appended claims. Accordingly, the specification is to be regarded in an illustrative rather than a restrictive sense. For example, specific water-soluble hydroxyacids, and combinations thereof with other mineral acids, other than those specifically exemplified or mentioned, or in different proportions, falling within the claimed parameters, but not specifically identified or tried in a particular application to transfer metals and/or amines into the aqueous phase, are within the scope of this invention. Similarly, it is expected that the inventive compositions will find utility as metal and phosphorus transfer compositions for other fluids besides crude oil emulsions. 

1. A method of transferring reactive phosphorus species from a hydrocarbon phase to a water phase in a refinery desalting process comprising: adding to wash water, an effective amount of a composition to transfer at least a portion of the reactive phosphorus species from a hydrocarbon phase to a water phase, the composition comprising at least one water-soluble hydroxyacid selected from the group consisting of gluconic acid, C₂-C₄ alpha-hydroxy acids, poly-hydroxy carboxylic acids, thioglycolic acid, chloroacetic acid, polymeric forms of the above hydroxyacids, poly-glycolic esters, glycolate ethers, and ammonium salt and alkali metal salts of these hydroxyacids, and mixtures thereof; adding the wash water to hydrocarbon to create an emulsion; and resolving the emulsion into hydrocarbon phase and an aqueous phase using electrostatic coalescence, where at least a portion of the reactive phosphorus species is transferred to the aqueous phase.
 2. The method of claim 1 where in the adding of the composition, the composition additionally comprises a mineral acid.
 3. The method of claim 2 where in the adding of the composition, the composition further comprises down to about 1 wt. % water-soluble hydroxyacid; and up to about 20 wt. % mineral acid.
 4. The method of claim 2 where the amount of mineral acid is sufficient to lower the pH of the wash water to 6 or below.
 5. The method of claim 1 where in the adding of the composition, the water-soluble hydroxyacid is present in the emulsion in an amount ranging from about 1 about 10,000 ppm.
 6. The method of claim 1 where in the adding of the composition, the composition further comprises water or alcohol solvent.
 7. The method of claim 1 further comprising after adding the composition to the emulsion, heating the emulsion to a temperature above about 180° F. (about 82° C.).
 8. A method of transferring reactive phosphorus species from a hydrocarbon phase to a water phase in a refinery desalting process comprising: adding to wash water, an effective amount of a composition to transfer at least a portion of the reactive phosphorus species from a hydrocarbon phase to a water phase, the composition comprising a mineral acid and at least one water-soluble hydroxyacid selected from the group consisting of gluconic acid, C₂-C₄ alpha-hydroxy acids, poly-hydroxy carboxylic acids, thioglycolic acid, chloroacetic acid, polymeric forms of the above hydroxyacids, poly-glycolic esters, glycolate ethers, and ammonium salt and alkali metal salts of these hydroxyacids, and mixtures thereof, where the water-soluble hydroxyacid comprises from about 1 to about 100 wt. % of the composition and the composition further comprises a water or alcohol solvent; adding the wash water to hydrocarbon to create an emulsion and resolving the emulsion into hydrocarbon phase and an aqueous phase using electrostatic coalescence, where at least a portion of the reactive phosphorus species is transferred to the aqueous phase.
 9. The method of claim 8 where the amount of mineral acid is sufficient to lower the pH of the wash water to 6 or below.
 10. The method of claim 8 further comprising after adding the composition to the emulsion, heating the emulsion to a temperature above about 180° F. (about 82° C.).
 11. A treated hydrocarbon emulsion comprising: a hydrocarbon phase; a water phase; a composition in an amount effective for transferring ay least a portion of a reactive phosphorus species from the hydrocarbon phase to the water phase, the composition comprising a water-soluble hydroxyacid selected from the group consisting of gluconic acid, C₂-C₄ alpha-hydroxy acids, poly-hydroxy carboxylic acids, thioglycolic acid, chloroacetic acid, polymeric forms of the above hydroxyacids, poly-glycolic esters, glycolate ethers, and ammonium salt and alkali metal salts of these hydroxyacids, and mixtures thereof; and a mineral acid.
 12. The treated hydrocarbon emulsion of claim 11 where the composition further comprises: down to about 1 wt. % water-soluble hydroxyacid; and up to about 20 wt. % mineral acid.
 13. The treated hydrocarbon emulsion of claim 11 further comprising wash water and where the amount of mineral acid is sufficient to lower the pH of the wash water to 6 or below.
 14. The treated hydrocarbon emulsion of claim 11 where the water-soluble hydroxyacid is present in the emulsion in an amount ranging from about 1 to about 10,000 ppm.
 15. The treated hydrocarbon emulsion of claim 11 where the composition further comprises at least one additional component selected from the group consisting of a water or alcohol solvent, a corrosion inhibitor, a demulsifier, a scale inhibitor, metal chelants, wetting agents and mixtures thereof.
 16. The treated hydrocarbon emulsion of claim 11 where the hydrocarbon component contains more than 3 ppm of a reactive phosphorus species. 